TWI293346B - Method for forming spread nonwoven webs - Google Patents

Abstract

A new fiber-forming method, and related apparatus, and webs prepared by the new method and apparatus are taught. In the new method a) a stream of filaments is extruded from a die of known width and thickness; b) the stream of extruded filaments is directed through a processing chamber that is defined by two narrowly separated walls that are parallel to one another, parallel to said width of the die, and parallel to the longitudinal axis of the stream of extruded filaments; c) the stream of filaments passed through the processing chamber is intercepted on a collector where the filaments are collected as a nonwoven fibrous web; and d) a spacing between the walls of the processing chamber is selected that causes the stream of extruded filaments to spread before it reaches the collector and be collected as a web significantly wider in width than the die. Generally the increase in width is sufficient to be economically significant, e.g., to reduce costs of web manufacture. Such economic benefit can occur in widths that are 50, 100 or 200 or more millimeters greater in width than the width of the die. Preferably, the collected web has a width at least 50 percent greater than said width of the die. The processing chamber is preferably open to the ambient environment at its longitudinal sides to allow pressure within the processing chamber to push the stream of filaments outwardly toward the longitudinal sides of the chamber.

Description

1293346 玖, invention description: The technical field of fibrous non-woven fabrics is the traditional method of extruding a silk-forming material that is originally liquid into a filament flow. After the filament leaves the mold, it is processed (such as cooling and drawing) and then collected. Collect the filaments. The wire pattern collected in the collector is a fiber material that can be processed into a mesh or can be processed into such a mesh. A generally collected material or web width is about the same as the width of the extruded wire mold; the right to be - half mesh. The mold must also be in the half range. Because of the economic efficiency of the wide mesh car, the wide mold is generally used. Wide molds have the right to dry defects. For example, the mold is heated to assist in forming the fiber material through the mold; the wider the mold, the more heat is required. At the same time, the wide mold has a higher manufacturing cost and is less maintenance. In addition, the width of the collected web is despised, and the use of the mesh is changed, but it is inconvenient to adjust the size of the mold or the proportion of the mold in order to cope with such a change. Prior Art The present invention provides a method of making a fibrous nonwoven web that can be controlled or selected for a mesh for a purpose of 1 degree, and which is not equal to the width of the extruded web mold. In summary, the method of the present invention comprises a) wiping the filament flow from a known width and thickness of the mold; b) guiding the extruded filament flow through two longitudinal parallel, parallel mold widths, and parallel extruded filament flow longitudinal axis walls The processing chamber; C) collecting and processing the filaments of the non-woven fiber web; and # adjusting the width of the wall to the width selected by the output, and adjusting the width of the filament to a width different from the mold. Preferably, the desired width of the filament flow is substantially greater than the width of the mold, and the filament flow is expanded as it travels from the mold to the collector, #collected by the functional web. Generally, when T is collected, the width of the web is at least 5 〇 or 1 346 1293346 m above the width of the mold; and the width of the preferred web is at least 200 mm or more above the width of the mold. It is narrower, so it is more flexible. Preferably, the processing chamber is open to the environment at least along the longitudinal axis of a portion of its side walls. Moreover, the walls are preferably covered with each other in the direction of travel of the filaments to facilitate expansion of the extruded filament stream. In the drawings: Figure 1 is a schematic illustration of the method of the present invention for forming a nonwoven web. Figure 2 is a cross-sectional view of the apparatus of Figure 1 taken along the line. Figure 3 is an enlarged side elevational view of the processing chamber of the present invention, showing no installation of the chamber. Figure 4 is a top plan view of the processing and mounting member and assembly of Figure 3. Figure 5 is a top plan view of another possible apparatus for operating the present invention. Figure 6 is a cross-sectional view taken along line 6-6 of Figure 5. Figure 7 is a side elevational view of another portion of the apparatus available for use in the present invention. SUMMARY OF THE INVENTION Figure 1 shows an exemplary apparatus for operating the present invention. The fiber material is directed to the apparatus extrusion head or die 10, which is first passed through a feed hopper and melted at extruder 12. The pump 13 pumps the molten material to the extrusion head 1 〇. It is most commonly used as a flake or granular solid polymeric material. 苒忮力丹's face can be pumped, and other fiber-making liquids can also be used, such as polymer solutions. In the evening, 4 10 can be a traditional multi-well plate or a rotating group, _ generally contains regular arrangement > 1 hole as arranged in an in-line arrangement. The filaments b of the fiber-making raw material are extruded by the extrusion head: to a processing chamber or reducer 16. _The wire 15 travels to the reducer 16 and can be different. The external conditions can also be different. In general, 1293346 provides a cooling flow of air or other gas to the extruded wire 15 in a conventional manner and apparatus. In addition, the air or other gas stream may be heated to assist in drawing the filament stream (or other fluid) in one or more lanes 'eg, the first air stream i8a is blown laterally to the filament stream, which may be removed during extrusion. The bad gaseous substance or smoke is produced; and the second cooling air flow 18b completes the main cooling. Depending on the processing conditions used or depending on the desired product, the cooling air can be fully cured before the extruded filament 15 reaches the reducer 16. Others can also maintain the extruded wire before entering the regulator in a soft or molten state. Or when no cooling flow is used, the ambient air or other fluid between the extrusion head 1 and the regulator 16 can be used to change the medium in which the extruded wire enters the reducer. ... The filament 15 exits through the reducer 16 and is described in detail below. As illustrated in Figures 2 and 2, the filaments flow away and enter the collector 19 where the filaments, or finished fibers, are collected in a homogenous or non-homogenous, manageable mesh type of fibrous web. As shown and described in detail in Figure 2, the fiber or filament stream 15 is preferably expanded at a distance 21 from the reducer to the collector 19. The collector 19 is generally porous and has a gas draw 14 below the collection to assist in accumulating the fibers on the collector. The collected material 20 can be sent to other devices such as calenders, embossing stations, laminating machines, cutting machines, etc.; or can be wound around a storage wheel ^3 by driving wheels 22 (Fig. Before the thumb filaments or fibers pass through the processing chamber into the collector, the extruded filaments or rakes can have a number of processing steps not shown in Figure 1, such as re-drawing, spraying, and the like. The representative and preferred device of the representative preferred processing device or reducer 16 of the present invention comprises two movable half groups or sides 16a and 16b, between which the processing chamber 24 is defined; 16a and 16b are opposite sides. 60 and 61 form the wall of 1293346 of the chamber. The exemplary apparatus 16 adjusts the spacing between the parallel walls of the process chamber to achieve control of the width of the extruded filaments in accordance with the present invention. The degree of extrusion filament flow or fiber expansion can be controlled by adjusting the spacing between the walls 60 and 61 of the reducer or processing unit 16. Another advantage of this device is that it can be operated continuously in the case of high speed narrow machining gaps and where the fiber material still enters the processing chamber in a soft condition. These conditions often cause blockages or interruptions in prior art processing equipment. The expansion of the filament flow of the present invention can contribute to the ability to reduce the spacing of the walls of the processing chamber, at least in some cases narrower than those used in conventional direct web forming processing chambers. The inter-wall space creates pressure that extends the airflow to the allowable width of the processing chamber and pushes the ribbon out of the width. Fig. 4 is a schematic view showing the manner of adjusting the spacing of the walls 60 and 61 of the preferred reducer 16 in a different scale, showing the reducer and its mounting and supporting structure. As shown at the top of Figure 4, the reducer 16 processes or reduces the chamber 24 to a generally long or four-sided long hole with a lateral length of 25 (transverse to the wire traveler path or longitudinal axis and parallel to the extrusion). Head or mold 10 width). Although the reducer 16 is present in two sets, the function is a single device. The integrated type will be discussed below (the structures shown in Figs. 3 and 4 are representative, and the available structures may be different types). The walls 62 and 63 define the entrance to the reduction chamber 24 or the throat 24a. The inlet wall sections 62 and 63 are preferably curved at the entry end or surfaces 62a and 63a to mitigate the flow of air carried into the extruded filament 15. Wall segments 62 and 63 are joined to a body portion 28 and may have recessed regions 29 for creating a gap 30 between body portion 28 and wall segments 62 and 63. Air or other gas is introduced into the gap 30 through the tube 31, creating an air knife (i.e., a pressurized air flow indicated by arrow 32) that can pull in the direction of travel of the wire, increasing the speed of the wire, and further cooling the wire. The reducer body 28 has a curvature at 28a better than !293346 to alleviate the passage of air by the air knife 32 into the passage. The angle (α) of the reducer body surface 28b can be selected to determine the angle of action of the air knife through the flow through the regulator. The air knife does not need to be located in the near chamber entrance, and vice versa. , the reducer chamber 24 along the length of the # body reducer (longitudinal length of the longitudinal sleeve along the _ reduction chamber is called the axial length) may have a uniform gap width as shown in Figure 2, two reducer side or wall 6 〇, horizontal distance 33. In addition, as shown in Fig. 3, the gap thickness can be changed to the vertical length. Preferably, the reduction chamber is tapered toward the length of the outlet %, for example at an angle β. Such a narrowing 'or the gradual convergence of the walls 6〇 and 61 at a point downstream of the air knife' provides, in at least some embodiments of the invention, an extruded filament flow along and exiting the outlet of the regulator, and 4 19 mobile expansion. In the specific example of the 4 wounds of the present invention, the wall may be _ 乂 分 乂 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游 下游The extrusion head or mold 10 has a narrow width to meet the requirements of the present invention. At the same time, in some cases with moon peas, the reduction chamber is made up of flat acres. The width of the wall gap is all in the wall or the part is fixed. In all cases ^, 巧1 j T, the boundary 疋 reduction or the walls 60 and 61 of the processing chamber are considered to be parallel to each other, because 眛, , ,, in the soil ^, the length of the Shao, the full parallel is very small. In the transverse direction of the room, the preferred Beibei is fully parallel. As shown in Fig. 3, the wall segments 64 and 65 (each belonging to the walls 60 and 61) of the main segment of the « , * π boundary 疋 24 pass may be attached to the body region 28, and may be attached to the body region 28 Board 36. P causes the defined wall to contain a portion of the processing & m, to length 'can still be extended after length, such as generating a pumping force or a van der Waals. The length of the reduction chamber 24 can be adjusted to achieve different effects; in particular, it is a zombie 匕^, a smashing knives 32 and an outlet 34, sometimes referred to as a bucket length 35. The use of the age <length' to select the wall gap and the -10- 1293346 coverage of the wall can expand the filament flow. The exit can use a wave-folding surface, a c〇anda curved surface, and an unbalanced wall length to achieve the desired expansion, or the distribution of other fibers. Generally, the gap width, the length of the bucket, the shape of the chamber, and the like are matched with the processing materials and the desired effect processing mode. For example, a longer bucket length can be used to enhance the crystallinity of the finished filament. Process conditions need to be adjusted to process the extruded filaments into the desired fiber form. As shown in Fig. 4, the two walls 16a and 16b of the representative reducer 16 are supported by mounting blocks 37 attached to the linear bearings 38 of the rod 39. The bearing % is low-friction on the rod. The ball bearing is extended through the axial rod so that the side turns 6a and 16b are easy to approach or separate from each other. The support block 37 is attached to the reducer body",

Air flows from the supply pipe 41 through the cover 40 to the pipe 31 and the air knife 32. In this specific example, the cylinders 43& and 431) are respectively connected to the reducer cases 16a and 16b through the speed lever 44, and the clamping force is provided to push the both sides 16a and 16b toward each other. The clamping force is matched with other operating materials to balance the pressure in the chamber 24, and at the same time, the desired wall gap of the processing chamber is set as described below. In other words, the clamping force and the internal pressure of the regulator

The force pushing the side is balanced to better operating conditions. The filaments can be extruded through the regulator ' to complete the filament collection while the regulator parts are maintained in an established equilibrium or steady state while the reduction chamber or passage 24 is maintained in equilibrium or gap. Figure μ representative device starts and establishes the operation (that is, after the filament is established) the side of the regulator or the chamber wall will only move when the system is broken (sometimes the wall will move to get different flow widths). Because the wire breaks or the winding of the = 'this usually causes the pressure of the reduction chamber 24 to rise, because the delivery end or winding from the head wire is enlarged, causing partial blockage to the chamber 24. -11 - 1293346 The walls 16a and 16b are moved away from each other. At this end, the moving wire end can pass through the reducer, and the pressure is restored until it is interrupted. The force of the clamping force of the 尧 action causes the reducer side to return to the original position. 4 告3成碉减1: The booster is “droplet”, that is, granules::: the wire is disturbed and falls, or the extruded wire is deposited in the reduction chamber, or the previously deposited wire. + Tired, the demonstration reducer 16 one side of 16a and 16b, 4 a poor, not a face

= is "floating", that is, it can be moved in the direction of the ^ arrow. Preferably, the force that acts only on the side of the reducer in addition to the frictional force and the gravity: the pressure generated in the self-rolling cylinder and the reduction chamber 24. The clamping force outside the cylinder is also the same. Use, such as spring 'elastic material deformation, or bumps, to: :: provide control and change. take

The chamber wall can be moved in a variety of ways. For example, in addition to the separation of the walls of the processing chamber by the flow force, the chamber can be used as a servo mechanism by using a sensor (for example, by laser or thermal sensation to detect the blockage of the wall or the chamber), and if necessary, separate the wall position. . In another useful apparatus of the present invention, the side of the reducer or the chamber wall: one or both can be driven in a superimposed manner, such as a servo, an oscillator, or a super first wave drive. The number of repetitions can be adjusted within a certain range, for example, from at least 5,000 times per minute to 60,000 times per second. In addition, there is a way to use the difference between the pressure of the fluid in the processing chamber and the external force to drive the wall apart or to restore the stable position. Specifically, under stable operation, the pressure in the processing chamber (which is the sum of the number of forces acting on the spoon in the processing chamber), such as the processing chamber type, the position and design of the air knife, and the velocity of the liquid flowing into the reservoir, acts on the outside of the processing wall. Pressure balance. If the chamber pressure rises due to the interruption of the -12- 1293346 fiber processing process, one or both of the chamber walls are separated from each other until the interruption is aborted, when the process chamber pressure is less than the steady state (because the wall gap is greater than the steady state). Therefore, the environmental pressure acting on the chamber wall pushes the chamber wall until the pressure is balanced with the external pressure, resulting in an equilibrium state. However, under the control of the device and processing parameters, it is not easy to rely solely on the differential pressure action. In general, in addition to being able to move in time and sometimes float, the walls of the sample processing chamber generally have means to move them. The wall of this example can be viewed as being connected to a set of devices that can be adjusted to the desired position at any time. The mobile device can be any processing room feature or related setting, or just one of the operating conditions, or a combination of various movements that can cause the child to move the wall, such as avoiding fiber breaks during processing, and establishing or restoring the chamber stability. State action. In the embodiment of Figures 1-3, the gap 33 of the reduction chamber 24 interacts with the chamber pressure, or the straight liquid flow rate and liquid temperature. With the chamber pressure and the clamping force changing with the gap of the chamber, at a certain liquid flow rate, the narrower the gap, the higher the chamber pressure and the higher the cooling force. The clamping force is small to make the gap wide. Structurally, mechanical stops should be included in the reducer examples 16a and 16b to maintain minimum and maximum clearance. In one example, the cylinder 43a supplies a greater clamping force than the cylinder 43b, such as 43a using a piston having a diameter greater than 43b. This force difference causes the reducer side i6b to be a side wall that is easy to move when the operation is interrupted. This force difference is approximately equal and can compensate for the frictional forces that limit the movement of the bearing 38 on the rod 39. The stop mode can be located at a larger gas red 43& to limit the movement of the reducer side 16a to the reducer side 16b. Figure 4 is a non-standard stop mode, as a double rod cylinder of the cylinder 43a, wherein the second rod 46 has a screw 'extending out of the mounting plate 47, with a 48 ° adjustable stop mode of the adjustable cylinder position, for example By rotating the nut, the reduction chamber 24 - 13 - 1293346 can be aligned with the extrusion head 1 〇. Since the above-described rapid adjustment and reduction chamber side 1 and l6b modes are provided, the wire forming processing operation parameters can be increased. Conditions that have been discontinued in the past, for example, may cause interruptions in rewiring, as the specific example methods and devices are acceptable, and when the wire is broken, the action of the wire drawing end is generally automated. Therefore, high-speed operation that is easy to move into a wire break can be utilized. Similarly, narrow gaps can result in a concentration of air knives and a stronger force and speed through the reducer. Alternatively, the wire can be introduced into the reduction chamber in a more molten state, which is better for the fiber-powered cycle car because the chance of blocking the reduction chamber is greatly reduced. The reducer can be more or less away from the wiping head to control other conditions, such as entering the person to reduce the room temperature, the chamber wall of the reducer 16 is a single structure 'but can also be formed by each component Said rapid or floating action. Each (4) contains the connection method. The rubber 2 === holds the pressure in the processing chamber 24. In another arrangement, the wall of the processing chamber 24 is formed by the elastic sheet of the material, and the chamber is locally deformed (in the case of monofilament or tow breakage: or the deviation mode can be used for segmentation or elastic wall;)

♦ 4 pairs of Shao deformation, so that the wall and you Jin J cut into two to the original position. In addition, as described above, the wall is partially overlaid. Or if the pressure and the effect of the body force on the wall or the local area are stopped, the second (4) 'for example' is interrupted, and the interruption is stopped, and the wall is returned to the unmodified shape, and the T mr ητ is elastic. Or the continuity of the segmented wall; It is also possible to control the fluid pressure. The above shows that the reducer 16 shows that the walls 6G and 61 are movable to adjust or select the distance between 14 and 1293346. Similarly, the wall can also be moved during the above-described device operation to change the width of the collecting sheet without stopping the operation. For example, increasing the pressure on each of the cylinders and/or 43b of the regulator reduces the wall 6〇 to 61 to a smaller phase. At the same time, a mechanical gear can be used to prevent the walls 60 and 61 from crossing or bifurcing when the wire is near the exit of the processing chamber. Another simpler embodiment of the invention wherein the chamber wall is immovable and fixed at a position that achieves a certain width of the filament flow (e.g., the wall is secured by a selected spacer such that the spacing cannot be manually or automatically changed during operation). Figures 5 and 6 are exemplary demonstrations of wall movements that aid in the definition of a process chamber, particularly in the form of a pivot wall that adjusts the deflection angle of the wall adjacent the chamber outlet. The apparatus 70 shown in Figures 5 and 6 includes mounting brackets 71a and 71b that each pivotally support the reducer halves 72a and 72b on the needle 73. The needle 73 is rotatably extended to the support frames 7 and 74b, each of which is attached to the body portions 75a and 75b of the half portions 72a and 72b. Mounting brackets 71a and 7 are coupled to cylinders 76a and 76b than rods 85 that are slidable through support frame 86. The cylinder applies a clamping force to the semi-shorings 72a and 72b through the mounting brackets 71a and 71b, and is applied to the processing chamber 77 defined between the two halves of the reducer. The support frames 71a and 71b are attached to a mounting bracket 78 that is low-friction sliding on the rod 79. The adjustment of the pivoting device or the reducer half is shown in Figure 6, taken along line 6-6 of Figure 5 (plus wall segments 62' and 63,). Each of the adjustments of the apparatus shown includes a brake 80a or 80b, each associated to the frame 71a or 71b and the plate 81a or 8, corresponding to the plate 36 of FIG. The available brakes include a brake internal drive shaft 82a or 82b that is urged by the motor to advance or retract the shaft. The shaft moves through the plates 81a and 81b to pivot the device half along the needle 73. In the preferred embodiment of process chambers 24 and 77, as shown in Figures 3-6, the lateral ends of the chamber have no sidewalls. This means that the processing chamber is open to the outside environment of the device. Therefore, the flow of the gas -15- 1293346 into the gas or gas stream can expand the processing chamber side under room pressure. Similarly, air or other gases can be drawn into the chamber. Similarly, the chamber fibers can also scatter outward as they approach the chamber exit. Such deployment - as described above, facilitates the collection of fibrous material for the collector. Preferably, the total length of the whole silk is increased by the length of the jade chamber (as shown in Fig. 2, line 15_, so that the collected mesh fibers have a more uniform sentence property. For example, the fiber can have a similar degree of reduction and similar fiber size, and the processing device Or reduce the crying wide yield (refer to the solid line 16 in Figure 2) can be wider than the wiper head or mold 1Q, in order to match the fiber processing room travel. Other examples of 'fiber flow can be expanded outside the wider processing room (Figure 2 Flow 15, shown by the dashed line of the processing device 16'. If the expansion is sufficient to cause a poor change in fiber properties, the fibrous material may be trimmed so that the fiber-woven nonwoven web that is passed through the processing chamber to the collector retainer will be completed. However, because the extrusion head extrudes the fiber into the collector, only a small part passes through the processing chamber (the main wire is drawn and the wire diameter is reduced before the wire enters the processing chamber and leaves the processing chamber), and the person who goes through the processing room is not serious. Affects the degree of fiber. The width of the collected mesh can be obtained from the control parameters in the fiber processing, including the wall spacing of the processing chamber. The finished mesh is a functional network (although other processing such as bonding, stretching, etc. may be required), That is, the properties of the collected fibers can be substantially uniform in width, which is sufficient for functional purposes. Generally, the basis weight of the finished web is not more than 30%, preferably not more than 1% by weight. However, the mesh can also produce special properties. Including more qualitative differences, and including paragraphs that can be cut from the collecting mesh to have different properties. In terms of economy, it is preferred to make a finished mesh having a width larger than the width of the wire extrusion die. The increased width can be affected by the above parameters, such as processing. Between the chamber walls ^, -16 - 1293346 and other such as the width of the collection net, the length of the reducer, and the distance from the outlet of the reducer to the collector. Some net widths increased by 50 mm, which is more than 1 增加. 〇mm, preferably increased by 200 mm or more. The latter increase has considerable commercial benefits in widening the processing. The mesh 15 is occupied by the included angle (Fig. 2 angle γ), depending on the target width of the collection net and others such as reduction Depending on the parameters of the collector distance, the gamma angle of the stream 15 is at least 10 in terms of a general distance, and more is at least 15 or 20. In many instances of the invention, the finished product (ie, the collection network) Or collecting net trimming department At least 50% more than the width of the extrusion head or mold (refers to the effective width of the mold, ie the liquid portion of the extruded fiber). Figure 7 shows another device of the invention at the same point of view as Figure 2, with a sector The reduction of the 90' is advantageous for the processing of the silk flow. The processing chamber and the defined processing wall are expanded or widened along the length of the processing 1: the force acting on the wire in the processing chamber is uniform throughout the flow width. The flow expands as needed.

The adjustment of the set, corresponding to instant movement. The dimension effect, including the k-side movement as described above, is rotated by the adjustment machine. In other examples, the side walls are separated, 1293346 is attached to the chamber side, and the other portion is attached to the other chamber side. The two side walls are preferably repeated to limit the processing of the fibers into the processing chamber. Generally, the deflection is mainly for unfolding the collected filament flow, and also for forming a mesh narrower than the mold (for example, the mold width is 75% or 50% or less). The narrowing is done by controlling the wall spacing of the processing chamber and by accepting the narrowing direction of the wall of the filament. The process and apparatus of the present invention can be used to form a plurality of fibrous materials for the fibers. Regardless of organic polymers, or inorganic materials such as glass or ceramic materials. The most

Suitable for molten fiber raw materials, other conditions such as solution or suspension can also be used. Any fiber-forming organic blendstock can be used, including conventional polymers for making fibers such as polyacetam, polypropylene, polyethylene terephthalate, nylon, and uramine. Part of the polymer raw material which is difficult to be fiber-spun or melt-blown can be used here, including amorphous polymers such as cycloolefins (the high melt viscosity limit is used in traditional direct extrusion techniques), bulk copolymers, Phenylethylene polymers and adhesives (including pressure sensitive and hot melt). The specific polymers listed here are only examples, and other materials may be used. In particular, this

The inventive fiber-forming process can be carried out at a lower temperature than conventional direct extrusion techniques, with more advantages. The fibers may also be formed by blending the raw materials, and include a plurality of materials which may be added to the additives such as materials or colorants. Bicomponent fibers, such as core-skin, or side-by-side, "fibers" can be prepared ("two-component" here contains two or more components). In addition, 'different raw materials can be squeezed from different pores of the extrusion head at the same time. A mesh of mixed fibers. In other specific embodiments of the present invention, other original sheets may be added before the fibers are prepared according to the present invention or when the fibers are collected. For example, -18- 1293346 fiber can be used in accordance with the US Department of Science and Technology, but other profiles are also available. Depending on the selected operation: the degree of melting from the molten state to the solid state before entering the regulator, the second is: it is quite continuous or substantially discontinuous. The orientation of the fiber polymer chain is influenced by parameters such as the degree of solidification, the airflow of the air knife into the second and the temperature, the axial length, the gap width and the shape (since the shape can affect the special fiber obtained by the processing device)

Cl: mesh. As with some collections..., the fibers are broken, = connected, 'either entangled with each other or with other fibers, or by impacting the walls of the processing chamber: a segment of the Si fiber segment, ie a broken fiber segment' and entanglement or deformation In the fiber: fiber 2 is the interrupted fiber segment, more often referred to as the 'fiber end"; these are the ends of the unaffected fiber length 'even if entangled or changed: both, the shape of the cut ball,) But usually in the fiber == is less than 300 microns straight to the end of the fiber usually, especially broken or radiant, so that the tail end is wrapped around itself or other fibers. This fiber is adjacent to other fibers, such as by the fiber tail The end is combined with the adjacent protons from the homogeneity of the king. The processing of the broken fibers produces a unique property that can be used in the present invention to achieve fiber continuity. Such fiber ends do not appear in the collection mesh of the worker A (for example When the fiber material is made into the curing process, it will not occur. Individual fibers are entangled in the processing chamber, taken or interrupted' or may be entangled with other fibers due to the deviation of the processing chamber wall or processing, or even Still in the molten state, but even 21- 1293346 has this In the case of if 'wire processing will not be interrupted. The result is a considerable amount of fiber ends measured in the collection mesh, or interrupted fiber segments in the discontinuity of the fiber. Interrupts generally occur in or after the processing chamber, and the fibers are generally subjected to pulling force. Function, so the fiber has tension when it is spliced or deformed. The fracture or entanglement causes the tension to stop, the fiber end shrinks and increases the diameter. At the same time, the fracture end freely moves with the fluid flow in the process, at least In some cases, the tail end is formed into a radial shape and entangled with other fibers. The analysis of the fiber tail end and the middle section gives the crystallinity of the two. The polymer chain at the end of the fiber is generally oriented, but different middle segments. Degree. Different orientations give different crystal ratios, and crystal types, or other crystal structures. This difference can cause different properties. Generally, &, when properly calibrated by differential scanning calorimetry (DSC) evaluation of the present invention When the fiber ends and the middle section, the fiber tail and the middle section will be different from each other. Generally, the heat conversion will appear in the test instrument (0·Γ(:), because the fiber middle section and the fiber tail end The mechanism of the action is different. For example, when the experiment can observe that the 'thermal conversion may have the following difference ··丨) glass transition temperature, the middle section can be slightly higher than the tail end temperature, and this feature will be high with the middle part of the fiber. Obviously; 2) When observed, the cold crystallization temperature and the peak area measurement value in the cold crystallization will be lower in the segment than in the tail end, and 3) the middle melting point temperature Tm of the fiber will be higher than the Tm ' or the nature of the tail end. Synthesize various multiple endothermic minimums (that is, the multi-melt strips represent different melting points of different molecular regions, and the degree of crystal structure is different), and the middle section of the fiber is melted in the middle of the fiber. There are different parameters such as one or more glass transition temperatures, cold crystallization temperatures, and at least 〇.5 bite °c melting point difference in the middle section of the fiber. -22· 1293346 has the advantage of a larger fiber end mesh, which may include a It is easier to soften the substance to increase the mesh bonding; and the radiation type can increase the homogeneity of the mesh. EXAMPLES Examples In the apparatus shown in Figure 1, the different polymers listed in Table 1 were made into a fibrous web. The specific components and operating conditions of the device are different and are also listed in Table 1. The extrusion die used in each case had a width of 4 inches (about 10 cm). Table 1 also lists the properties of the finished fibers, including the width of the nonwoven web collected. Examples 1-22 and 4L43 were made of polypropylene; Examples 1-13 were prepared with a melt flow coefficient (ΜΠ) 400 polypropylene (Exxon 35〇5G), and Example I4 was prepared with an MFI of 30 polypropylene (Fina 3868). Example 15_22 was prepared with ΜΠ 70 70 polypropylene (Fina 3860) and Examples 42-43 were prepared with MFI 400 polypropylene (Fina 3960). The polypropylene density was 0.91 g/cc. Examples 23-32 and 44-46 were prepared from polyethylene terephthalic acid; Examples 23-26, 29-32, and 44 were prepared from PET having a viscosity (IV) of 0.61 (3M 651000), and Example 27 was prepared from PET having an IV of 0.36. Example 28 was prepared from PET having an IV of 0.9 (a high molecular weight PET that can be used as a high-coiled fiber, such as Crystar 0400 from Dupont Polymer), and Examples 45 and 46 were prepared as PETG (Ax45-produced by Paxon Polymer Company, Baton Rouge, LA). 004). The PET density is 1.35 and the PETG density is about 1.30. Examples 33 and 41 were prepared as nylon 6 polymers having an MFI of 130 and a density of 1.15 (Ultramid PA6 B_3, BASF). Example 34 was prepared as a polystyrene having a density of 15.5 and a density of 1.04 (Nova Chemicals Crystal PS 3510). Example 35 Preparation of a polyurea having a enthalpy of 37 and a density of 1.2 (Morton PS_440-200). -23- 1293346 Example 36 was prepared with polyethylene having an MFI of 30 and a density of 0.95 (Dow 6806). Example 37 was prepared as a block copolymer containing 13% phenethyl hydrazide and 87% ethylene butene copolymer, having a enthalpy of 8, and a density of 0.9 (Shell Kraton G1657). Example 38 is a two-component core-sheath fiber, the core (89%) being the phenethyl hydrazine used in Example 34, and the sheath (11%) being the copolymer used in Example 37. Example 39 was prepared from two fibers of adjacent fibers of polyethylene (Exxact 40, Exxon Chemicals, 30), (36%) and a pressure sensitive adhesive (64%). The adhesive contained 92% isooctylpropionic acid, 4% phenelzine, and 4% propionic acid, viscosity 0.63, supplied by a Bonnot adhesive extruder, all °/〇 are percentage by weight. Each of the fibers of Example 40 was a single component, but fibers of different polymer compositions, polyethylene of Example 36, and polypropylene used in Examples 1-13 were used. The extrusion head has 4 rows of holes, 42 rows of each row, and the extrusion head is supplied with the same row of holes as the difference between the two polymers to achieve the A-B-A··. arrangement. The web of Example 47 was prepared solely from a pressure sensitive adhesive which was used in one of the components of Example 39, and a Bonnot adhesive extruder. In Examples 42 and 43, the coil spring was used to replace the cylinder that pushes the movable side or wall of the reducer. The spring of Example 42 deviated 9.4 mm on each side during operation. The spring constant of the spring is 4.38 Newtons/Amm. The clamping force of each spring is 41.1 Newtons. The spring of Example 43 was offset by 2.95 mm on each side during operation, with a spring constant of 4.9 N/mm and a clamping force of 14.4 Newtons. The extrusion head of Example 44 was a meltblown mold having a hole diameter of 38 mm and a hole center distance of 1.02 mm. The holes are 101.6 mm long. The primary meltblown air temperature was 370 °C, and the combined air knife was introduced at a flow rate of 〇45 cubic meters per minute (CMM) through a 203 mm wide air knife on each side of the hole. 1293346, Example 47 pneumatic rolling bead oscillator is about 2 times per second, connected to each movable side or wall, the cylinder remains stationary, the positive adjustment chamber is below the extrusion head, and when there is pressure accumulation forced side separation , can restore the reduction side to the initial position I. The operation of the oscillator, in the state of the oscillator operation, produces a smaller amount of viscous adhesive attached to the regulator wall than in the absence of oscillator operation. The clamps of Examples 7 and 37 are added as 〇, but the balance between the chamber and ambient air pressure creates a gap between the chamber walls and returns the active position to the initial position after any interruption. The polymer forming the fibers of each case is heated as listed in Table ( (temperature is taken from the outlet of the extruder 12 near the pump 13), and the polymer is converted into the m-state polymer to the extruder according to the flow rate shown in Table i. hole. The extruder head typically has four rows of holes, however the number of perforations, the aperture, and the length to diameter ratio of the holes are also different, as listed in the table. Example 1 2 5-7 ′ 14-24 ′ 27, 29-32, 34 and 36-40 each has 42 holes, for a total of 168 holes. In the other examples other than Example 44, for every 21 holes, a total of holes were discussed. The parameters of the reducer also vary as shown in the table, including the air knife gap (size 30 in Figure 3), the angle of the decelerator king (Fig. 32α), the air temperature through the regulator, the cooling air flow rate, and the cylinder Reducer clamping force; the total amount of air through the regulator (in actual cubic meters per minute, or ACMM; about half of the listed values through each air knife 32), · reducer upper and lower clearance (Figure 3 Dimensions" and 34); reducer bucket length (Figure 3 size 35); mold exit edge to reducer distance (Figure 17 size 17); and reducer exit column collector distance (Figure i size 21). The length of the air knife is about 120 mm (the direction of the groove length of Figure 4) is about 120 mm; the main body of the reducer 28 is vented by a concave die of about 152 mm. The wall of the main body of the reducer is different in length. Example 1- In 5,8_25,27_28,33_35 and 37-47, the wall mold length is 254 mm; in Examples 6, 26, 29_32 and 36, it is 406 mm; and in Example 7, it is about 127 mm. -25- 1293346 Recorded, including average fiber diameter, imaged using a scanning electron microscope, and used in Windows 1 of the University of Texas Health Science Center in San Antonio .28 version of UTHSCSA IMAGE Tool imaging analysis program (1995-97 patent). Image magnification 500 to 1000 times, depending on fiber size. Collecting fiber appearance silk speed is calculated by the following formula, V outside * = 4 Μ / ρ π φ 2, where Μ For each pore polymer flow rate, gram per cubic meter, p is the polymer density, and df is measured in meters to determine the average fiber diameter. The fiber's solidity and elongation fracture are taken from a single fiber that is enlarged and placed on a paper holder. The fiber breaking strength was measured by ASTM D3822_90 method. The average breaking strength and elongation fracture were obtained from 8 fibers. The viscosity was calculated by the average breaking strength and the average fiber Dani value obtained from the fiber diameter and the polymer density. The cut sample contains the fiber end portion, that is, the fiber segment obtained by breaking or extending the discontinuity, and also includes the middle fiber segment, that is, the main unaffected portion of the fiber. The sample is analyzed by different scanning calorimeters, The DSCTM analysis of the Model 2920 from TA Instruments in New Castle, DE, has a heat rate of 4 ° C per minute and a tolerance of 636.636 ° C for 60 seconds. The melting point of the middle section; Table 1 shows the maximum melting point peak of the middle and the end of the fiber on the DSC chart. Although some of the examples do not detect the melting point difference between the middle and the tail, there are still other differences, such as the glass transition temperature. The fiber mid- and tail-end samples were also analyzed by X-ray diffraction. Using Bruker's micro-diffuser (Madison, WI's Bmker AXS), copper Κ alpha radiation, and -26- 1293346 HI-STAR 2D scattering position The sensor collects data. The diffractometer has a 300 micron aligner and a graphite projection beam monochromator. The X-ray generator consists of a rotating anode surface set at 50 kV and 100 mA operation with copper as the stem. The data was collected with an emission spectrum of 60 minutes and a center of the detector at 0° (2Θ). The Brukei* GADDS data is used to analyze the software correction detector sensitivity and spatial irregularity. The corrected data was averaged in azimuth, reduced to x-y and density values in the scattering angle (2Θ) group, and analyzed by ORIGINTM number analysis software distribution (provided by Microcal Software, Inc., Northhampton, MA) to evaluate its crystallinity. Gaussian peak mode was used to analyze the distribution of each crystalline meal and amorphous meal. In some data sets, a single amorphous strip does not represent a completely amorphous scan density. In these cases, an extra wide maximum is utilized to fully represent the measured non-crystalline scan density. The crystallinity coefficient is calculated from the ratio of the crystalline meal area to the total scan pupil area in the range of 6° to 36° (2Θ) scanning angle. A single value represents 100% crystallinity and zero represents a completely amorphous material. The values obtained are listed in Table 1. In Examples 1, 3, 13, 20, and 22, which are made of polypropylene, the X-ray analysis shows the difference between the middle and the tail, and the tail includes the β crystal form, measured at 5.5 angstroms. The draw area ratio is determined by dividing the total fiber cross-sectional area by the cross-sectional area of the die hole, and taking the average fiber diameter. The production index is also calculated. Table 1 Example No. 1 2 3 4 5 6 7 8 9 l Polymer PP PP PP PP PP PP PP PP PP MFI/IV 400 400 400 400 400 400 400 400 400 400 Melting temperature (C) 187 188 187 183 188 188 188 188 180 188 Number of holes 168 168 84 84 168 168 168 84 84 84 Polymer flow rate (g/hole/min) 1.00 1.00 1.00 1.04 1.00 1.00 1.00 0.49 4.03 1.00 Aperture (mm) 0.343 0.508 0.889 1.588 0.508 0.508 0.508 0.889 0.889 0.889 Small hole L/D 9.26 6.25 3.57 1.5 6.25 6.25 6.25 3.57 3.57 3.57 -27- 1293346 Air gap (mm) 0.762 0.762 0.762 0.762 0.762 0.762 0.762 0.381 1.778 0.381 Reducer body angle (degrees) 30 30 30 30 30 30 30 20 40 20 Reducer air temperature (C) 25 25 25 25 25 25 25 25 25 25 Cooling air volume (ACMM) 0.44 0.35 0.38 0.38 0.38 0.37 0 0.09 0.59 0.26 Clamping force (Newton) 221 221 59.2 63.1 148 237 0 23.7 63.1 43.4 Reducer air volume (ACMM) 2.94 2.07 1.78 1.21 2.59 2.15 2.57 1.06 >3 1.59 Reducer clearance (top) (mm) 4.19 3.28 3.81 4.24 3.61 2.03 3.51 2.03 5.33 1.98 Reducer clearance (lower ) (mm) 2.79 1.78 2.90 3 .07 3.18 1.35 3.51 2.03 4.60 1.88 bucket length (mm) 152.4 152.4 152.4 152.4 76.2 228.6 25.4 152.4 152.4 152.4 Die to reducer distance (mm) 317.5 317.5 317.5 317.5 317.5 304.8 304.8 304.8 304.8 914.4 Reducer to collector distance ( Mm) 609.6 609.6 609.6 609.6 609.6 609.6 609.6 609.6 609.6 304.8 Average fiber straight root (μ) 10.56 9.54 15.57 14.9 13.09 10.19 11.19 9.9 22.26 14.31 --Γ* ------ Appearance wire speed (m/min) 12600 15400 5770 6530 8200 13500 11200 6940 11400 6830 Viscosity one (g/Dani) 2.48 4.8 1.41 1.92 2.25 2.58 2.43 2.31 0.967 1.83 Extension before break (%) 180 180 310 230 220 200 140 330 230 220 Pulling area ratio 1050 2800 3260 11400 1510 2490 2060 8060 1600 3860 Melting point · Medium (°C) 165.4 165.0 164.1 164.1 165.2 164.0 164.3 165.2 164.3 165.4 Second peak (°C) Melting point - tail (°C) 163.9 164.0 163.4 163.4 163.2 162.5 164.0 163.3 164.3 163.2 Second peak (°C) Crystallinity Index - Medium 0.44 0.46 0.42 0.48 0.48 0.52 0.39 0.39 0.50 0.40 Yield Index gm/hole.min2 12700 15500 5770 6760 8240 13600 11300 3380 45800 6^30 Net width (mm) N/M 508 584 292 330 533 102 267 203 241 Fiber flow containing angle (γ) (degrees) N/M 37 43 18 21 39 a 15 10 26 Table 1 Example No. ϋ 12 13 14 15 16 17 18 J9 Polymer ΡΡ FI ΡΡ ΡΡ ΡΡ ΡΡ ΡΡ ΡΡ ΡΡ MFI/IV 400 400 400 30 70 70 70 70 70 Melting temperature Zhan (C) 190 196 183 216 201 201 208 207 206 Small Number of holes 84 84 84 168 168 168 168 168 168 -28- 1293346 Polymer flow rate (g/hole/min) 1.00 1.00 1.00 0.50 1.00 0.50 0.50 0.50 0.50 Aperture (mm) 0.889 0.889 1.588 0.508 0.343 0.343 0.343 0.343 0.343 Small hole L /D 3.57 3.57 1.5 3.5 9.26 3.5 3.5 3.5 3.5 Air knife gap (mm) 0.381 1.778 0.762 1.270 0.762 0.762 0.762 0.762 0.762 Reducer body angle (degrees) 20 40 30 30 30 30 30 30 30 Reducer air temperature (c 25 25 121 25 25 25 25 25 25 Cooling Air Volume (ACMM) 0 0.59 0.34 0.19 0.17 0 0.35 0.26 0.09 Clamping force (Newton) 27.6 15.8 55.2 25.6 221 27.6 27.6 27.6 27.6 Reducer air volume (ACMM) 0.86 1.19 1.25 1.24 2.84 0.95 0.95 1.19 1.54 Reducer Room (上) (mm) 2.67 6.30 3.99 5.26 4.06 7.67 5.23 3.78 3.78 Reducer clearance (bottom) (mm) 2.67 6.30 2.84 4.27 2.67 7.67 5.23 3.33 3.33 bucket length (mm) 152.4 76.2 152.4 152.4 152.4 152.4 152.4 152.4 152.4 Reducer distance (mm) 101.6 127 317.5 1181.1 317.5 108 304.8 292.1 292.1 Reducer to collector distance (mm) 914.4 304.8 609.6 330.2 609.6 990.6 787.4 800.1 800.1 Average fiber diameter (μ) 18.7 21.98 14.66 16.50 16.18 19.20 17.97 14.95 20.04 Appearance wire speed (m/min) 4000 2900 6510 2570 5370 1900 2170 3350 1740 Viscosity (g/Danny) 0.52 0.54 1.68 2.99 2.12 2.13 2.08 2.56 0.87 Extension before break (%) 150 100 110 240 200 500 450 500 370 Pull area ratio 2300 1600 12000 950 450 320 360 560 290 Melting point - medium (°C) 162.3 163.9 164.5 162.7 164.8 164.4 166.2 163.9 164.1 Second peak (°C) 167.3 164.4 Melting point-tail (°C) 163.1 163.4 164.3 163.5 163.8 163.7 164.0 163.9 163.9 Second peak (°C) 166.2 Crystallinity index - medium 0.12 0.13 0.46 0.53 0.44 0.33 0.43 0.37 0.49 Yield index gm/hole.min2 4000 2900 6500 1280 5390 950 1080 1680 870 Mesh width (mm) 292 114 381 254 432 127 165 279 406 Fiber flow containing angle (γ) (degrees) 12 2.4 26 26 30 1.4 4.6 13 22 Table 1 performance example number 20 21 22 23 24 25 26 27 Polymer PP PP PP PET PET PET PET PET MFI/IV 70 70 70 0.61 0.61 0.61 0.61 0.36 Melting temperature (C) 221 221 221 278 290 281 290 290 Small hole number 168 168 168 168 168 84 84 168 Polymer flow rate (g/hole/min) 0.50 0.50 0.50 1.01 1.00 0.99 0.99 1.01 Aperture (mm) 0.343 0.343 0.343 0.343 0.508 0.889 1.588 0.508 Small hole L/D 3.5 3.5 3.5 3.5 3.5 3.57 3.5 3.5 -29- 1293346 Air knife gap (mm) 0.762 0.762 0.762 1.778 1.270 0.762 0.381 1.270 Reducer body angle (degrees) 30 30 30 20 30 30 40 30 Reducer air temperature (C) 25 25 25 25 25 25 25 25 Cooling air volume (ACMM) 0.09 0.30 0.42 0.48 0.35 0.35 0.17 0.22 Clamping force (Newton) 27.6 150 17.0 3.9 82.8 63.1 3.9 86.8 Reducer air volume (ACMM) 1.61 >3 1.61 2.11 2.02 2.59 0.64 2.40 Reducer clearance (top) (mm) 3.78 3.78 3.78 4.83 5.08 5.16 2.21 5.03 Clearance (bottom) (mm) 3.33 3.35 3.35 4.83 3.66 4.01 3.00 3.86 bucket length (mm) 152.4 152.4 152.4 76.2 152.4 152.4 228.6 152.4 Die to reducer distance (mm) 508 508 685.8 317.5 533.4 317.5 317.5 127 Reducer to Collector distance (mm) 584.2 584.2 431.8 609.6 762 609.6 609.6 742.95 Average fiber diameter (μ) 16.58 15.73 21.77 11.86 10.59 11.92 13.26 10.05 Appearance wire speed (m/min) 2550 2830 1490 6770 8410 6580 5320 9420 Viscosity (g/丹尼 1.4 1.9 1.4 1.2 5.9 3.6 3.0 3.5 Extension before break (%) 210 220 250 40 30 40 50 20 Ratio of draw area 430 480 250 840 2300 5600 1400 2600 Melting point - medium (°C) 165.9 163.9 165.7 260.9 259.9 265.1 261.0 256.5 Second peak (°C) 167.2 258.5 267.2 — 258.1 268.3 Melting point-tail (°C) 164.1 164.0 163.7 257.1 257.2 255.7 257.4 257.5 Second peak (°C) 253.9 254.3 268.7 253.9 · Crystallinity index - medium 0.5 0.39 0.40 0.10 0.20 0.27 0.25 0.12 Yield index gm/hole.min2 1270 1410 738 6820 8400 6520 5270 9500 Net width (mm) 203 406 279 N/M 254 N/M 216 457 The fiber flow contains angles (γ) ( 10 29 23 N/M 11 N/M 11 27 Table 1 continued example number 28 29 30 31 32 33 34 35 Polymer PET PET PET PET PET Nylon PS Urethane MFI/IV 0.85 0.61 0.61 0.61 0.61 130 15.5 37 Melting temperature ( C) 290 282 281 281 281 272 268 217 Number of holes 84 168 168 168 168 84 168 84 Polymer flow rate (g/hole/min) 0.98 1.01 1.01 1.01 1.01 1.00 1.00 1.98 Aperture (mm) 1.588 0.508 0.508 0.508 0.508 0.889 0.343 0.889 Small hole L/D 3.57 6.25 6.25 6.25 6.25 6.25 9.26 6.25 Air gap (mm) 0.762 0.762 0.762 0.762 0.762 0.762 0.762 0.762 Reducer body angle (degrees) 30 30 30 30 30 30 30 30 Reducer air temperature ( C) 25 25 25 25 25 25 25 25 -30- 1293346

Cooling air volume (ACMM) 0.19 0 0.48 0.48 0.35 0.08 0.21 0 Clamping force (Newton) 39.4 82.8 86.8 82.8 82.8 39.4 71.0 86.8 Reducer air volume (ACMM) 1.16 2.16 2.16 2.15 2.15 2.12 2.19 >3 Reducer clearance ( () 3) 3.86 3.68 3.67 3.58 3.25 4.29 4.39 4.98 Reducer clearance (bottom) (mm) 3.10 3.10 3.10 3.10 2.64 3.84 3.10 4.55 bucket length (mm) 76.2 228.6 228.6 228.6 228.6 76.2 152.4 76.2 Die to reducer distance (mm) 317.5 88.9 317.5 457.2 685.8 317.5 317.5 317.5 Reducer to collector distance (mm) 609.6 609.6 609.6 482.6 279.4 831.85 609.6 609.6 Average fiber diameter (8) 12.64 10.15 10.59 11.93 10.7 12.94 14.35 14.77 Appearance wire speed (m/min) 5800 9230 8480 6690 8310 6610 5940 9640 Viscosity (g/Danny) 3.6 3.1 4.7 4.1 5.6 3.8 1.4 3.3 Extension before breakage (%) 30 20 30 40 40 140 40 140 Ratio of draw area 16000 2500 2300 1800 2300 4700 570 3600 Melting point -Medium (°C) 268.3 265.6 265.3 262.4 261.4 221.2 23.7? Second peak (°C) 257.3 257.9 269.5 218.2 9 Melting point-tail (°C) 254.1 257.2 257.2 257.4 257.4 219.8 ? Two peaks (°C) 268.9 268.4 * * 氺一__ __ Crystallinity index - medium 0.22 0.09 0.32 0.35 0.35 0.07 0 0 Yield index gm/hole.min2 5690 9320 8560 6740 8380 6610 5940 19100 Net width (mm) 305 559 559 711 457 279 318 279 Fiber flow containing angle (γ) (degrees) 19 41 41 65 65 12 20 17 Table 1 continued example number 36 37 38 39 40 41 42 Polymer PE Bl. CopoL PS/copol. PE/PSA PE/PP Nylon PP MFI/IV 30 8 15.5/8 30/.63 30/400 130 400 Melting temperature (C) 200 275 269 205 205 271 206 Number of holes 168 168 168 168 168 84 84 Polymer flow rate (g/ Hole/min) 0.99 0.64 1.14 0.83 0.64 0.99 2.00 Aperture (mm) 0.508 0.508 0.508 0.508 0.508 0.889 0.889_ Small hole L/D 6.25 6.25 6.25 6.25 6.25 6.25 6.25 Air gap (mm) 0.762 0.762 0.762 0.762 0.762 0.762 0.762 H Body angle (degrees) 30 30 30 30 30 30 30 Seat air temperature (C) 25 25 25 25 25 25 25 Cooling air volume (ACMM) 0.16 0.34 0.25 0.34 0.34 0.08 0.33 Clamping force (Newton) 205 0.0 27.6 23.7 213 150 41.1, reducer air volume (ACMM) 2.62 0.41 0.92 0.54 2.39 >3 >3

-31- 1293346 Reducer clearance (top) (mm) 3.20 7.62 3.94 4.78 3.58 4.19 3.25 reducer clearance (bottom) (mm) 2.49 7.19 3.56 4.78 3.05 3.76 2.95 bucket length (mm) 228.6 76.2 76.2 76.2 76.2 76.2 76.2 Mold to reducer distance (mm) 317.5 666.75 317.5 330.2 292.1 539.75 317.5 Reducer to collector distance (mm) 609.6 330.2 800.1 533.4 546.1 590.55 609.6 Average fiber diameter (8) 8.17 34.37 19.35 32.34 8.97 12.8 16.57 Appearance wire speed (m/ Min) 19800 771 4700 1170 11000 6700 10200 Viscosity (g/Danny) 1.2 1.2 1.1 3.5 0.8 Extension before breakage (%) 60 30 100 50 170 Ratio of draw area 3900 220 690 250 3200 4800 2900 Melting point - medium (°C 118.7 165.1 Second wave punch (°C) 123.6 Melting point-tail (°C) 122.1 164.5 Second peak (°C) Crystallinity index - medium 0.72 0 0 0.36 0.08 0.43 Yield index gm/hole.min2 19535 497 5340 972 7040 6640 20400 Mesh width (mm) N/M 89 406 N/MN/M 279 305 Fiber flow containing angle (γ) (degrees) N/M 22 11 11 17 19 Table 1 continued example number 43 44 45 46 47 Polymerization PP PET PETG PETG PSA MFI/IV 4 00 0.61 >70 >70 0.63 Melting temperature (C) 205 290 262 265 200 Small hole number 84 氺氺84 84 84 Polymer flow rate (g/hole/min) 2.00 0.82 1.48 1.48 0.60 Aperture (mm) 0.889 0.38 1.588 1.588 0.508 Small hole L/D 6.25 6.8 3.5 3.5 3.5 Air gap (mm) 0.762 0.762 0.762 0.762 0.762 Reducer body angle (degrees) 30 30 30 30 30 Reducer air temperature (C) 25 25 25 25 25 Cooling Air volume (ACMM) 0.33 0 0.21 0.21 0 Clamping force (Newton) 14.4 98.6 39.4 27.6 氺氺氺 Reducer air volume (ACMM) 2.20 1.5 0.84 0.99 0.56 Reducer clearance (top) (mm) 4.14 4.75 3.66 3.56 6.30 Reducer clearance (bottom) (mm) 3.61 4.45 3.38 3.40 5.31 bucket length (mm) 76.2 76.2 76.2 76.2 76.2 -32- 1293346

Mold to reducer distance (mm) 317.5 102 317 635 330 Reducer to collector distance (mm) 609.6 838 610 495 572 Average fiber diameter (8) 13.42 8.72 19.37 21.98 38.51 Appearance wire speed (m/min) 15500 10200 3860 3000 545 Viscosity (g/Dani) 3.6 2.1 1.64 3.19 Pre-extension (%) 130 40 60 80 A draw area ratio 4388 1909 6716 5216 1699 Melting point-medium (°C) 164.8 257.4 Second peak (°C 254.4 Melting point-tail (°C) 164.0 257.4 Second wave punching (°C) 254.3 Crystallinity index - Medium 0.46 <0.05 0 0 Yield index gm/hole.min2 31100 8440 5700 4420 330 Net width (mm) 191 381 203 254 N/M fiber flow containing angle (γ) (degrees) 8 19 10 17 N/M * complex value ** melt blown valve *** tube wall vibration diagram at 200 cycles / sec 10 Extrusion head or die 11 Feed hopper 12 Extruder 13 Pump 14 Gas extraction device 15 Wire flow 16 Reducer 16a, 16b Reducer side a, b 17 Axial length 18a First gas flow 1293346 18b Second Gas stream 19 collector 20 fibrous material 21 distance 22 drive roller 23 storage fluid wheel 24, 77 Processing chamber 25 Transverse length 26 Longitudinal shaft 27, 90 Bucket 28 Body portion 29 Recessed area 30 Clearance 31 Pipeline 32 Air knife 33 Pitch thickness 34 Outlet opening 35 Bucket length 37, 78 Mounting block 38 Bearing 39, 79, 85 Rod 40, 72 Half 41 Supply pipe 43, 76 Cylinder 1293346 44, 80 Connecting rod 46 Bolt rod 47 Mounting plate 48 Nut 50 Wall spacing 60, 61 Side wall 62 to 65 Wall section 70 Unit 71 Frame 73 Needle 74 Support block 75 Main part 81 plate 82 drive shaft 86 support frame 89 expansion bucket

Claims (1)

April) Patent Application No. 3474: General Appropriation, Science and Technology, and the original version of the patent (1). The method of preparing a non-woven fabric, which includes & ) from - known wide production and: degree mold extrusion of the filament flow; b) guiding the extrusion filament flow through two close distances: the door is separated and mutually flat 'at the same time parallel to the width of the mold and parallel to the take-up wire - The processing chamber of the boundary; the illusion of a collector is accepted by the processing until the (silk mud) wire is collected by the non-woven fabric; and The width is at least 5 mm larger than the width of the mold. I. The method of claim 1, wherein the longitudinal side of the processing chamber defined by the two walls is open to the surrounding environment. I, as in the method of claim 1, wherein (4) The width in the direction of travel with the wire is greater than the upstream point at the downstream point of the wire travel. I. As in the method of claim 3, (4) processing at least the MM (four) long at least the Shao system is closed to the surrounding environment. The method of claim 1 of the patent scope, wherein the parallel The method of any one of the inventions, wherein the collecting I functional net is at least 100 mm larger than the width of the mold. The method of any of the items, wherein the collected functional network is at least 200 mm wider than the width of the mold. 8. The method of any one of clauses 5 to 5, wherein the width of the filament extends before entering the collector. The method according to any one of the preceding claims, wherein the width of the wire is at least twice the width of the mold before entering the collector. 1〇·If the patent application scope (1) In any one of the methods, the silky non-woven fabric formed by the silk flow 85451-960413.doc 1293346 has a thickness of at least 5 mm, hard/gram. The private reaction is at least 10 ml U. As claimed in the first to fifth patents In any of the methods, the extrusion silkiness of the laboratory is controlled so that the wire collector collects when the force is combined: the K fruit can be automatically I2. The processing room is defined in the first to fifth patent applications. One of the walls, automatic 1/: a method in which at least the soil is automatically moved closer to or away from the other wall and is controlled by a mobile device that provides an immediate action when the filament passes. 13. The method of any one of claims 5 to 5, The processing crucible includes an air knife that can apply a pulling force to the processing direction of the processing chamber. The method of any one of the preceding claims, wherein the extruded filament flow system is at least 8 inches per minute. The method of the present invention, wherein the filament flow rate is passed through the processing chamber, wherein the extruded filament flow passes through the filament speed of i 〇〇〇〇m per minute. The process of any one of the preceding claims, wherein the extruded filament stream passes through the processing chamber at an apparent filament speed sufficient to provide a production index of at least 9 Torr. 85451-960413.doc